WO2020194284A1 - Système de dessalement capable de produire de l'hydrogène - Google Patents

Système de dessalement capable de produire de l'hydrogène Download PDF

Info

Publication number
WO2020194284A1
WO2020194284A1 PCT/IB2020/054866 IB2020054866W WO2020194284A1 WO 2020194284 A1 WO2020194284 A1 WO 2020194284A1 IB 2020054866 W IB2020054866 W IB 2020054866W WO 2020194284 A1 WO2020194284 A1 WO 2020194284A1
Authority
WO
WIPO (PCT)
Prior art keywords
water
concentrated water
unit
concentrated
chlorine
Prior art date
Application number
PCT/IB2020/054866
Other languages
English (en)
Korean (ko)
Inventor
홍승관
김정빈
최종문
박기호
Original Assignee
고려대학교 산학협력단
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 고려대학교 산학협력단 filed Critical 고려대학교 산학협력단
Priority to EP20776475.4A priority Critical patent/EP3848331A4/fr
Publication of WO2020194284A1 publication Critical patent/WO2020194284A1/fr

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/06—Energy recovery
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
    • B01D61/364—Membrane distillation
    • B01D61/3641—Membrane distillation comprising multiple membrane distillation steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/58—Multistep processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/043—Details
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/46104—Devices therefor; Their operating or servicing
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
    • C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/34—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis
    • C25B1/46—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis in diaphragm cells
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/50—Processes
    • C25B1/55—Photoelectrolysis
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/02—Process control or regulation
    • C25B15/023—Measuring, analysing or testing during electrolytic production
    • C25B15/025—Measuring, analysing or testing during electrolytic production of electrolyte parameters
    • C25B15/029—Concentration
    • C25B15/031—Concentration pH
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/08—Specific process operations in the concentrate stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/26—Further operations combined with membrane separation processes
    • B01D2311/2642—Aggregation, sedimentation, flocculation, precipitation or coagulation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/26—Further operations combined with membrane separation processes
    • B01D2311/2684—Electrochemical processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/36—Energy sources
    • B01D2313/367—Renewable energy sources, e.g. wind or solar sources
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F2001/5218—Crystallization
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/009—Apparatus with independent power supply, e.g. solar cells, windpower or fuel cells
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/46—Apparatus for electrochemical processes
    • C02F2201/461—Electrolysis apparatus
    • C02F2201/46105—Details relating to the electrolytic devices
    • C02F2201/4616—Power supply
    • C02F2201/46165—Special power supply, e.g. solar energy or batteries
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/133—Renewable energy sources, e.g. sunlight
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy

Definitions

  • the present invention relates to a desalination system capable of producing hydrogen, and more particularly, to a desalination system capable of producing hydrogen capable of producing hydrogen gas, which is a future energy source, from concentrated water discharged as wastewater during the existing seawater desalination process.
  • desalination is a combination of desalination to remove minerals and deionization to remove ions, and is also referred to as desalination desalination.
  • Seawater desalination methods include reverse osmosis and electrodialysis using a special membrane, evaporation method of desalination by converting seawater into steam (multi-stage flash evaporation method, multiple utility method, vapor compression method), and other methods such as refrigeration and solar heat.
  • evaporation and reverse osmosis are mainly used for seawater desalination.
  • the seawater desalination facility by the reverse osmosis method filters ionic substances dissolved in seawater by a semipermeable membrane (membrane) through which ionic substances dissolved in water are almost excluded and pure water passes.
  • FIG. 1 schematically shows a seawater desalination process chart by reverse osmosis.
  • the seawater desalination process by the reverse osmosis method is divided into a pretreatment process, a reverse osmosis process, and a post-treatment process.
  • seawater is supplied to the reverse osmosis process unit 20 after foreign substances and/or suspended matters are filtered out in the pretreatment unit 10.
  • Seawater introduced into the reverse osmosis process unit 20 is separated into concentrated water in which salt is concentrated and product water from which salt is removed through a reverse osmosis membrane under a high pressure of 42 to 60 bar.
  • the product water from which the salt has been removed is supplied to the product water storage tank 30.
  • the produced water is used after sterilization with chlorine gas.
  • Concentrated water is the water remaining after production water is generated from seawater. Therefore, the concentration of salt is very high and it is under high pressure. Concentrated water passes through the energy recovery unit, delivers high pressure to the influent, and is discharged to the sea with the pressure reduced.
  • the chemical supply unit 50 injects a pH adjusting solution and an anti-scaling agent into the reverse osmosis process unit 20.
  • Seawater contains substances such as boron or silica, but the concentration of boron and silica in the water produced through the seawater desalination process should be low. In particular, since boron is toxic, it must be removed below an appropriate concentration.
  • the reverse osmosis process removes carbonate ions and bicarbonate ions, so the alkalinity of the product water is low. Therefore, after passing through the reverse osmosis process in the form of carbon dioxide by lowering the pH of the influent water, the alkalinity is recovered by raising the pH in the post-treatment process. Sodium hydroxide is used at this time. Accordingly, in the seawater desalination process according to the conventional reverse osmosis method, chemicals such as sodium hydroxide and anti-scaling agents are continuously consumed.
  • production water is supplied through a pipe network. At this time, in order to prevent contamination of the production water due to the occurrence of microorganisms.
  • the production water should be chlorinated.
  • the chlorine tank 40 is connected to the storage tank 30 to provide chlorine gas to the storage tank 30 to disinfect the product water. Accordingly, additional costs are incurred for disinfection using chlorine.
  • concentrated water is being discharged without being utilized in the post-treatment process.
  • the concentrated water subjected to the reverse osmosis process has a very high salinity. If concentrated water is discharged to the sea without diluting it, it has a negative impact on the marine environment.
  • Patent Document 1 Korean Patent Registration No. 10-1526299 discloses a plant-forward osmosis hybrid desalination system and method.
  • the present invention utilizes concentrated water discharged as wastewater in the existing seawater desalination process to produce hydrogen gas, which is a future energy source, water treatment of seawater with fresh water, and chemicals required to produce hydrogen gas, such as chlorine, sodium hydroxide, and It aims to provide a desalination system capable of producing hydrogen that can produce hydrochloric acid itself.
  • the present invention charges electric energy to the seawater battery unit through electrolysis of influent water, and generates hydrogen gas through the water treatment process of concentrated water, so that renewable energy can be efficiently utilized and at the same time as an energy carrier in various fields. It aims to provide a desalination system capable of producing available hydrogen.
  • An object of the present invention is to provide a fresh water system capable of producing hydrogen capable of producing hydrogen gas using concentrated water discharged from a process of desalination treatment of seawater without the addition of a high concentration of NaCl solution.
  • the present invention absorbs carbon dioxide (CO 2 ) when discharging the seawater battery to remove divalent cations in concentrated water, and divalent cations contained in concentrated water adhere to the distillation membrane or membrane during the evaporation process of concentrating the concentrated water. It aims to provide a desalination system capable of producing hydrogen that can prevent scaling that occurs due to the problem.
  • CO 2 carbon dioxide
  • the present invention produces hydrogen that can reduce the energy consumption of the reverse osmosis process by desalination of the diluted influent water, which has a lower salinity as the salt escapes by generating chlorine gas while electrolyzing the influent during charging of the seawater battery unit. It aims to provide a possible freshwater system.
  • An object of the present invention is to provide a freshwater system capable of producing hydrogen capable of preventing destruction of marine ecosystems by crystallizing high-salt concentrated water into salt and discharging high-concentrated concentrated water to the sea.
  • a desalination system capable of producing hydrogen includes: a desalination process unit in which influent water is treated with production water and concentrated water through a reverse osmosis process; And a chlorine-alkali processing unit in which an internal space is partitioned into an anode unit to which concentrated water is supplied and a cathode unit to which production water is supplied, wherein the chlorine-alkali processing unit uses solar electric energy, and uses concentrated water as an electrolyte in the anode unit. It is preferable to generate chlorine gas from the salt of concentrated water through a chemical reaction, and to generate hydrogen gas and sodium hydroxide through a chemical reaction at the cathode with the produced water as an electrolyte.
  • the desalination system capable of producing hydrogen according to an embodiment of the present invention is installed between the desalination process unit and the chlorine-alkali process unit, and concentrates the concentrated water to a salinity higher than that of the concentrated water through an evaporation process. And, it is preferable to further include a concentration process unit for water treatment with the second product water from which the salt has been removed from the concentrated water.
  • the freshwater system capable of producing hydrogen according to an embodiment of the present invention is installed between the concentration processing unit and the chlorine-alkali processing unit, and sodium hydroxide is added to the second concentrated water supplied from the concentration processing unit, through a precipitation reaction. It is preferable that the second concentrated water further comprises a precipitation step for water treatment with the third concentrated water from which the divalent cations have been removed.
  • the freshwater system capable of producing hydrogen according to an embodiment of the present invention is installed between the precipitation process unit and the chlorine-alkali process unit, and by injecting hydrochloric acid into the third concentrated water supplied from the precipitation processing unit, the third concentrated water is It is preferable to further include a concentrated water pretreatment unit for water treatment with the fourth concentrated water having a pH lower than that of the third concentrated water.
  • the chlorine-alkali processing unit receives the fourth concentrated water from the concentrated water pretreatment unit to the anode unit, and generates chlorine gas from the fourth concentrated water through a chemical reaction at the anode unit using the fourth concentrated water as an electrolyte. It is preferable to discharge the diluted concentrated water from which the salt has escaped from the concentrated water to the concentrated water pretreatment unit.
  • a freshwater system capable of producing hydrogen includes a product water storage tank for storing product water supplied from a desalination process unit; A chlorine tank that stores chlorine gas supplied from the anode part and is connected to the production water storage tank to supply chlorine gas to the production water storage tank; A hydrogen tank for storing hydrogen gas supplied from the cathode; And a NaOH tank that stores sodium hydroxide generated through a chemical reaction at the cathode and supplies sodium hydroxide to the product water flowing into the cathode, and chlorine gas is supplied to the production water storage tank to disinfect the product water.
  • Sodium hydroxide is preferable to adjust the pH of the product water flowing into the cathode.
  • a freshwater system capable of producing hydrogen includes a hydrochloric acid reaction unit that is individually connected to a chlorine tank and a hydrogen tank, and produces hydrochloric acid through a chemical reaction between the supplied chlorine gas and hydrogen gas; And a hydrochloric acid tank in which hydrochloric acid is stored and connected to the concentrated water pretreatment unit to supply hydrochloric acid to the concentrated water pretreatment unit.
  • the produced water in the cathode, is electrolyzed into hydrogen gas and hydroxyl group (OH-) to produce hydrogen gas, and sodium ions and hydroxyl group (OH-) decomposed in the salt of concentrated water It is preferable to produce sodium hydroxide by chemical reaction.
  • the desalination process unit while the reverse osmosis process is performed, the influent water is separated into production water and concentrated water by high pressure;
  • an energy recovery unit connected to the reverse osmosis process unit and the concentration process unit, receiving concentrated water from the reverse osmosis unit, transferring the pressure of the concentrated water to the inlet water, and providing the concentrated water with reduced pressure to the concentration unit.
  • the fresh water system capable of producing hydrogen according to an embodiment of the present invention further includes a concentrated water crystallizer for receiving the diluted concentrated water discharged from the chlorine-alkali processing unit and crystallizing the diluted concentrated water.
  • a freshwater system capable of producing hydrogen includes a seawater battery unit that generates chlorine gas from salts of the influent water by causing a chemical reaction with the influent water as an electrolyte during charging, and 1 Influent water treatment unit for water treatment with concentrated water;
  • the first concentrated water is supplied, the first concentrated water is treated with the second concentrated water and the second produced water through a concentration process, and the second concentrated water is subjected to a chemical reaction as an electrolyte to form chlorine gas from the salt of the second concentrated water.
  • the influent water treatment unit includes: a seawater battery unit provided with a charging unit and a discharge unit; And a desalination processing unit connected to the charging unit to receive the diluted inflow water having a diluted concentration as salt escapes from the inflow water, and water-treating the diluted inflow water into the first production water and the first concentrated water through a reverse osmosis process.
  • the seawater battery unit receives the first concentrated water and carbon dioxide to the discharge unit when discharging, and removes divalent cations from the first concentrated water through a chemical reaction between the first concentrated water and carbon dioxide. It is desirable.
  • the desalination unit for hydrogen production receives the first concentrated water from which the divalent cations have been removed, and concentrates it through a concentration process, so that the second concentrated water and the second concentrated water are higher in salinity than the first concentrated water.
  • the concentrated water treatment unit further includes a concentrated water pretreatment unit for adjusting the pH of the second concentrated water by adding hydrochloric acid to the second concentrated water.
  • a product water storage tank connected to an influent water treatment unit and a desalination unit for hydrogen production and storing the first product water and the second product water;
  • a chlorine tank for storing chlorine gas supplied from the charging unit and the anode unit;
  • a hydrogen tank for storing hydrogen gas supplied from the cathode;
  • a NaOH tank that stores sodium hydroxide generated through a chemical reaction at the cathode, wherein chlorine gas is supplied to the production water storage tank to disinfect the product water, and sodium hydroxide is the second product water flowing into the cathode. Is added to, it is preferable to adjust the pH of the second production water.
  • the present invention can produce hydrogen gas, which is a future energy source, from concentrated water discharged as wastewater during the existing seawater desalination process, and can produce chlorine, sodium hydroxide, and hydrochloric acid consumed in the desalination process.
  • hydrogen energy obtained by hydrogen gas obtained from a chlorine-alkali process unit can be utilized as a driving source of a hydrogen bus and a fuel cell.
  • the present invention can continuously produce produced water (eg, fresh water) and hydrogen energy from salt-containing influent (eg, seawater).
  • produced water eg, fresh water
  • salt-containing influent eg, seawater
  • the present invention heats concentrated water using solar heat, and uses electric energy produced from solar energy as a driving source of the chlorine-alkali process unit, thereby reducing the operating cost of a desalination system capable of producing hydrogen.
  • the chlorine gas generated in the chlorine-alkali processing unit can be used for disinfection of production water, thereby reducing the cost of bad products consumed during disinfection.
  • the present invention supplies the diluted concentrated water discharged from the chlorine-alkali processing unit to the concentrated water pretreatment unit without discharging it to the sea, thereby reducing the destruction of the ecosystem due to the existing concentrated water having high salinity discharged to the sea.
  • an aqueous sodium hydroxide solution which is a by-product generated during the discharge of the chlorine-alkali process, can be used as a water treatment chemical to adjust the pH in the chlor-alkali process, thereby reducing the cost of chemicals.
  • the present invention can self-produce hydrochloric acid from chlorine gas and hydrogen gas produced in the chlorine-alkali process unit, thereby reducing the cost of chemicals consumed during water treatment of concentrated water.
  • hydrogen gas In order to produce hydrogen gas using seawater, a high concentration of NaCl concentrated water is required.
  • hydrogen gas can be produced by using the concentrated water discharged from the process of desalination of seawater without the addition of a high concentration NaCl solution. .
  • the present invention generates chlorine gas while electrolyzing the influent water during charging of the seawater battery unit, thereby desalination of the diluted influent water having a lower salinity through the reverse osmosis process, thereby reducing the energy consumption of the reverse osmosis process.
  • the present invention absorbs carbon dioxide (CO 2 ) during discharge of the seawater battery to remove divalent cations such as Ca 2+ or Mg 2+ ions in the concentrated water, and is contained in the concentrated water during the evaporation process of concentrating the concentrated water. It is possible to prevent scaling caused by attachment of the divalent cations to the distillation membrane. For this reason, the present invention can omit a nanofiltration process and an antiscalant process necessary for removing divalent ions before concentrating the concentrated water. In addition, the present invention prevents scaling generated in the distillation film or the membrane during the evaporation process, thereby extending the service life of the concentrated water treatment unit.
  • CO 2 carbon dioxide
  • the salt by crystallizing high-salt concentrated water into salt, the salt can be recycled or treated as waste.
  • the present invention can prevent the destruction of the marine ecosystem due to the high concentration of concentrated water being discharged to the sea.
  • FIG. 1 schematically shows the configuration of a seawater desalination process according to the prior art.
  • FIG. 2 is a block diagram of a desalination system capable of producing hydrogen according to a first embodiment of the present invention.
  • FIG. 3 is a flow chart of water treatment of the desalination process unit according to the first embodiment of the present invention.
  • FIG. 4 is a flow chart of water treatment of the concentration process unit according to the first embodiment of the present invention.
  • FIG. 5 is a flow chart of water treatment of the precipitation process unit according to the first embodiment of the present invention.
  • FIG. 6 is a water treatment flow chart of the concentrated water pretreatment unit according to the first embodiment of the present invention.
  • FIG. 7 is a flow chart of water treatment of a chlorine-alkali process unit according to a first embodiment of the present invention.
  • FIG. 8 is a view for explaining a desalination system capable of producing hydrogen according to a second embodiment of the present invention.
  • 9 and 10 are views for explaining the charging/discharging and desalination process of the seawater battery unit according to the second embodiment of the present invention.
  • FIG. 11 is a view for explaining a water treatment process of a desalination unit for hydrogen production according to a second embodiment of the present invention.
  • FIG. 12 is a view for explaining a process of generating hydrogen gas while passing through a chlorine-alkali process unit in a second embodiment of the present invention.
  • a desalination system capable of producing hydrogen according to an embodiment of the present invention includes: a desalination process unit in which influent water is treated with production water and concentrated water through a reverse osmosis process; And a chlorine-alkali processing unit in which an internal space is partitioned into an anode unit to which concentrated water is supplied and a cathode unit to which production water is supplied, wherein the chlorine-alkali processing unit uses solar electric energy, and uses concentrated water as an electrolyte in the anode unit. It is characterized in that chlorine gas is generated from the salt of concentrated water through a chemical reaction, and hydrogen gas and sodium hydroxide are generated through a chemical reaction at the cathode with the produced water as an electrolyte.
  • the present invention is to produce hydrogen gas, which is a future energy source, from concentrated water discharged as wastewater in the existing seawater desalination process, and to self-produce chlorine, sodium hydroxide, and hydrochloric acid consumed in the desalination process.
  • a desalination system 100 capable of producing hydrogen includes a desalination process unit 110, a concentration process unit 120, a precipitation process unit 130, a concentrated water pretreatment unit 140, a chlorine-alkali process unit ( 150), NaOH tank 161, hydrogen tank 163, chlorine tank 165, hydrochloric acid reaction unit 170, hydrochloric acid tank 180, production water storage tank 190 and concentrated water crystallization unit 198.
  • a desalination process unit 110 includes a concentration process unit 120, a precipitation process unit 130, a concentrated water pretreatment unit 140, a chlorine-alkali process unit ( 150), NaOH tank 161, hydrogen tank 163, chlorine tank 165, hydrochloric acid reaction unit 170, hydrochloric acid tank 180, production water storage tank 190 and concentrated water crystallization unit 198.
  • the desalination process unit 110 is a device that treats water with salt-containing product water (for example, fresh water) from which salt is removed while influent (for example, sea water) is subjected to a reverse osmosis process and concentrated water in which salt is concentrated.
  • salt-containing product water for example, fresh water
  • influent for example, sea water
  • the desalination process unit 110 includes a high pressure pump 111, a reverse osmosis process unit 112, and an energy recovery unit 113.
  • the reverse osmosis process unit 112 is a device in which a reverse osmosis process is performed.
  • the reverse osmosis process unit 112 may perform the reverse osmosis process several times according to the degree to which salt is removed from the influent water according to the type of production water (drinking water, agricultural water, industrial water).
  • the energy recovery unit 113 is a device that receives the concentrated water discharged from the reverse osmosis process unit 112 and recovers the pressure of the concentrated water.
  • the water treatment process of the desalination process unit 110 will be described as follows.
  • the high-pressure pump 111 pumps influent water from the sea to form a reverse osmosis process unit 112.
  • the reverse osmosis process unit 112 separates the influent water into production water and concentrated water through a reverse osmosis process.
  • the reverse osmosis process used in the seawater desalination process is a known technique, and a detailed description thereof will be omitted herein.
  • the product water discharged from the reverse osmosis process unit 112 is stored in the product water storage tank 190.
  • the pressure of the high-pressure concentrated water is recovered in the energy recovery unit 113.
  • the concentrated water is supplied to the concentration process unit 120 after energy is recovered by the energy recovery unit 113.
  • seawater has a salinity of 3.5%.
  • Concentrated water that has passed through the desalination process unit 110 has a salinity of approximately 6%.
  • a high-concentration sodium chloride solution of about 25% is required as the influent, and in this embodiment, the process of concentrating the concentrated water prior to performing the chlorine-alkali process is preceded.
  • the concentration process unit 120 is installed between the desalination process unit 110 and the precipitation process unit 130.
  • the concentration process unit 120 concentrates the salt concentration of the concentrated water to a high concentration through an evaporation process.
  • the concentration process unit 120 may concentrate the concentrated water with a salinity of 6% to approximately 25% of the concentrated water.
  • the concentration process unit 120 includes a concentrated water tank 121, a heating device 122 and an evaporation unit 124.
  • the concentrated water tank 121 is a tank in which concentrated water passed through the energy recovery unit 113 is stored. In the concentrated water tank 121, the concentrated water is heated by solar heat or a separate heating device 122. The heated concentrated water is supplied to the evaporation unit 124.
  • the evaporation unit 124 separates the concentrated water into the second product water and the second concentrated water through an evaporation process.
  • the evaporation process may be performed by selecting any one of a film evaporation process (MD), a multi-stage evaporation process (MSF), or a multiple effect evaporation process (MED) according to the flow rate of the concentrated water introduced into the evaporation unit 124.
  • MD film evaporation process
  • MSF multi-stage evaporation process
  • MED multiple effect evaporation process
  • the second production water is supplied to the production water storage tank 190 from the concentration process unit.
  • a part of the second production water may be supplied to the cathode of the chlorine-alkali process unit 150.
  • the second product water is mixed with sodium hydroxide solution and then used as an electrolyte for the cathode.
  • the second concentrated water is concentrated water concentrated to a higher salinity than that of the concentrated water.
  • the second concentrated water is supplied from the concentration processing unit to the precipitation processing unit 130.
  • the precipitation process unit 130 is installed between the concentration process unit 120 and the concentrated water pretreatment unit 140.
  • the precipitation process unit 130 receives the second concentrated water from the concentration process unit 120 and treats the chemical with sodium hydroxide to generate a precipitation reaction of the second concentrated water.
  • some of the sodium hydroxide is produced by the chlorine-alkylation process unit.
  • the second concentrated water is treated with a third concentrated water from which divalent cations (Ca 2+ , Mg 2+, etc.) have been removed by a precipitation reaction with sodium hydroxide.
  • the third concentrated water is concentrated water from which divalent cations have been removed from the second concentrated water.
  • the third concentrated water is discharged from the precipitation process unit 130 and is supplied to the concentrated water pretreatment unit 140.
  • the concentrated water pretreatment unit 140 is installed between the precipitation process unit 130 and the chlorine-alkali process unit 150.
  • the concentrated water pretreatment unit 140 injects hydrochloric acid into the third concentrated water supplied from the precipitation process unit, and water-treats the third concentrated water with a fourth concentrated water having a pH lower than that of the third concentrated water.
  • the pH of the concentrated water is exposed before flowing into the chlorine-alkali processing unit 150, and the concentrated water reacts with the chlorine gas in the chlorine-alkali processing unit 150 to generate hypochlorous acid (HClO) and other compounds. Can be prevented.
  • hypochlorous acid HlO
  • the concentrated water pretreatment unit 140 receives the third concentrated water, the diluted concentrated water, and hydrochloric acid, and discharges the fourth concentrated water.
  • the third concentrated water is concentrated water having a higher pH than the fourth concentrated water.
  • the diluted concentrated water is concentrated water having a lower salinity than the fourth concentrated water.
  • hydrochloric acid is a chemical used to adjust the pH of concentrated water.
  • hydrochloric acid is produced from chlorine gas and hydrogen gas generated in the chlorine-alkali process unit 150. Hydrochloric acid is supplied from the hydrochloric acid tank 180 to the concentrated water pretreatment unit 140.
  • the internal space of the chlorine-alkali process unit 150 is divided into an anode portion 151 and a cathode portion 155 by a separator.
  • An anode 152 is installed on the anode part 151.
  • a cathode 156 is installed on the cathode 155.
  • the anode 152 and the cathode 156 are electrically connected.
  • the chlorine-alkali process unit 150 electrolyzes concentrated water through solar electric energy to produce chlorine gas at the anode unit 151 and produces hydrogen gas and sodium hydroxide at the cathode unit 155.
  • the anode part 151 is provided with a first fluid inlet 151a, a first fluid outlet 151b, and a first gas outlet 151c.
  • the first fluid inlet 151a is connected to the precipitation process unit 130 and is a passage through which the fourth concentrated water is introduced.
  • the first fluid outlet 151b is a passage through which the diluted concentrated water is discharged.
  • the first fluid outlet 151b is connected to the precipitation process unit 130.
  • the first gas outlet 151c is a passage through which chlorine gas is discharged.
  • the first gas outlet 151c is connected to the chlorine tank 165.
  • the cathode part 155 is provided with a second fluid inlet 155a, a second fluid outlet 155b, and a second gas outlet 155c.
  • the second fluid inlet 155a is a passage through which the product water mixed with the sodium hydroxide solution is introduced.
  • the second fluid inlet 155a is a passage connected to the discharge passage of the second product water of the concentration process unit 120 to receive the second product water. At this time, sodium hydroxide solution is also supplied from the NaOH tank. Alternatively, the second fluid inlet 155a may be connected to the product water storage tank 190 to receive product water from the product water storage tank 190.
  • the second fluid outlet 155b is a passage through which sodium hydroxide solution is discharged.
  • the second fluid outlet 155b is connected to the NaOH tank 161.
  • the second gas discharge port 155c is a passage through which hydrogen gas is discharged.
  • the second gas outlet 155c is connected to the hydrogen tank 163.
  • the power source used may be solar electric energy produced by solar energy.
  • the fourth concentrated water stored in the anode part 151 is an electrolyte of the anode 152 and causes a chemical reaction according to the following equation (1).
  • the salt (NaCl) contained in the fourth concentrated water is separated into sodium ions and chlorine gas.
  • Sodium ions pass through the separation membrane partitioning the anode part 151 and the cathode part 155, and move from the anode part 151 to the cathode part 155.
  • Chlorine gas is collected and stored in the chlorine tank 165. Chlorine gas is supplied to the production water storage tank 190, and can be used as a chemical to disinfect the production water. In addition, chlorine gas is supplied to the hydrochloric acid reaction unit 170 and may be used as a raw material for producing hydrochloric acid.
  • the present invention can disinfect the water produced by using the chlorine gas produced in the chlorine-alkali processing unit 150 without using a separate chlorine chemical, and by producing hydrochloric acid itself, it is consumed to adjust the pH of the water treatment process. It can reduce the cost of chemical treatment.
  • diluted concentrated water As the salt is removed from the fourth concentrated water by the chemical reaction according to Equation (1), the salinity is lowered.
  • concentrated water having a lower salinity than the fourth concentrated water is referred to as diluted concentrated water.
  • the diluted concentrated water is discharged from the anode part 151 to the concentrated water pretreatment part 140.
  • the diluted concentrated water is not discharged to the sea as it is, but is discharged to the concentrated water pretreatment unit 140, thereby preventing environmental pollution due to the diluted concentrated water being discharged to the sea as it is.
  • the pH of the second product water is adjusted by sodium hydroxide, and is provided to the negative electrode part 155.
  • the second production water is fresh water treated by the concentration process unit 120.
  • the second product water is the electrolyte of the cathode 156.
  • Sodium hydroxide is produced by the chlorine-alkali process unit 150.
  • the second product water is used as an electrolyte, and the product water is electrolyzed into hydrogen gas and hydroxyl group (OH-) to produce hydrogen gas.
  • the formula for producing hydrogen gas is formula (2).
  • the hydrogen gas is stored in the hydrogen tank 163 through the second gas outlet 155c. Hydrogen gas can be used as hydrogen energy.
  • sodium hydroxide is produced by a chemical reaction between sodium ions decomposed in the salt of concentrated water and a hydroxyl group (OH-).
  • the formula for producing sodium hydroxide is Equation (3).
  • the sodium hydroxide solution is stored in the NaOH tank 161 through the second fluid outlet 155b.
  • Sodium hydroxide solution is used to adjust the pH of the fluid in the process of treating the influent water.
  • Sodium hydroxide is used as a chemical agent that adjusts the pH of the product water flowing into the negative electrode part 155 of the chlorine-alkali process part 150 described above.
  • sodium hydroxide is used as a chemical that adjusts the pH of concentrated water and/or produced water, such as the desalination process unit 110 and/or the precipitation process unit 130.
  • sodium hydroxide solution is added to the influent to increase the pH of the influent, thereby increasing the removal rate of specific substances such as boron or silica from the influent water passing through the reverse osmosis process, and carbon dioxide that has passed through the reverse osmosis process is converted into carbonate ions or bicarbonate.
  • Alkalinity can be recovered by turning into ions.
  • the present invention can prevent corrosion of a pipe network through which the product water flows by injecting an aqueous sodium hydroxide solution into production water having a low pH after mineral injection.
  • hydrochloric acid is produced by the following process.
  • the chlorine gas and hydrogen gas produced in the chlorine-alkali process unit 150 are supplied to the hydrochloric acid reaction unit 170, respectively.
  • the formula for producing hydrochloric acid is formula (4).
  • the hydrochloric acid produced in the hydrochloric acid reaction unit 170 is stored in the hydrochloric acid tank 180.
  • the present invention produces hydrochloric acid by itself through chlorine gas and hydrogen gas produced in the chlorine-alkali process unit 150, and uses it as a chemical agent to adjust the pH of concentrated water, which is consumed when operating a fresh water system capable of producing hydrogen. You can reduce the cost of chemicals.
  • the concentrated water crystallization unit 198 removes moisture from the diluted concentrated water through a crystallization process, and crystallizes the diluted concentrated water as salt (NaCl).
  • salt NaCl
  • the diluted concentrated water is heated, and the salt in the diluted concentrated water is crystallized while the water in the diluted concentrated water escapes as steam.
  • the crystallized salt (NaCl) can be recycled or treated as waste.
  • the present invention can prevent the destruction of the marine ecosystem due to the high concentration of concentrated water being discharged to the sea.
  • the desalination system 200 capable of producing hydrogen according to an embodiment of the present invention includes an influent water treatment unit 210, a desalination unit 230 for hydrogen production, a concentrated water crystallization unit 240, an energy supply unit. (250), product water storage tank (271), chlorine tank (273), hydrogen tank (275), and NaOH tank (277).
  • the influent water treatment unit 210 includes a seawater battery unit 211 and a desalination process unit 214.
  • the seawater battery unit 211 charges electric energy through an oxidation/reduction reaction of ions in the influent water. During discharge, electric energy may be used as an energy source of the desalination process unit 214.
  • the seawater battery unit 211 is composed of a charging unit 212 and a discharging unit 213.
  • the charging unit 212 is electrically connected to the energy supply unit 250.
  • the energy supply unit 250 generates new and renewable energy such as solar power generation, hydroelectric power generation, and wind power generation, and applies the generated electric energy to the charging unit 212.
  • Chlorine ions are oxidized to chlorine gas, collected in the charging unit 212, and stored in the chlorine tank 273. Sodium ions flow from the charging unit 212 to the discharge unit 213 through the separation membrane.
  • Chlorine gas may be used as a chemical to disinfect the first product water produced by the desalination process unit 214.
  • the present invention can self-produce chlorine gas consumed in disinfecting the first production water in the seawater battery unit 211, thereby reducing the cost of chemical treatment.
  • Salts in the influent are removed by electrolysis according to equation (1).
  • the influent water whose salinity is lowered through the filling process of the charging unit 212 will be referred to as diluted influent water.
  • the diluted inflow water is discharged from the charging unit 212 to the desalination process unit 214.
  • the desalination process unit 214 water-treats the diluted inflow water through a reverse osmosis process.
  • the diluted inflow water is treated with first production water and first concentrated water while passing through the desalination process unit 214.
  • the first production water is stored in the production water storage tank 271.
  • the first concentrated water is supplied to the discharge unit 213.
  • the first concentrated water has a higher salinity than the diluted influent water.
  • the reverse osmosis process may be performed several times depending on the degree to which salts are removed from the influent water depending on the type of first production water (drinking water, agricultural water, industrial water).
  • the reverse osmosis process used in the seawater desalination process is a known technique, and a detailed description thereof will be omitted herein.
  • the present invention generates chlorine gas while electrolyzing the influent water when charging the seawater battery unit 211, thereby desalination of diluted influent water having a lower salinity through a reverse osmosis process, and energy used to operate the reverse osmosis process. The amount can be reduced.
  • the first concentrated water and carbon dioxide are supplied to the discharge part 213.
  • the first concentrated water is one having a higher salinity than the influent water while passing through the desalination process unit 214.
  • divalent cations eg, Ca 2+ or Mg 2+ ions
  • carbon dioxide contained in the first concentrated water cause a chemical reaction, and the divalent cations are removed from the first concentrated water. do.
  • Carbon dioxide is reduced to carbonate ion CO 3 2- ).
  • Calcium ions (Ca 2+ ) react with carbonate ions (CO 3 2- ) and precipitate as calcium carbonate (CaCO 3 ).
  • Magnesium ions (Mg 2+ ) are chemically reacted with carbonate ions (CO 3 2- ) to precipitate as magnesium carbonate (MgCO 3 ).
  • divalent cations are removed from the first concentrated water through a chemical reaction between the first concentrated water and carbon dioxide.
  • sodium is oxidized to sodium ions, thereby increasing the salinity of the first concentrated water from which the divalent cations have been removed.
  • the present invention absorbs carbon dioxide (CO 2 ) when discharging the seawater battery unit 211 to remove divalent cations, such as calcium ions (Ca 2+ ) or magnesium ions (Mg 2+ ), in concentrated water.
  • divalent cations such as calcium ions (Ca 2+ ) or magnesium ions (Mg 2+ )
  • concentration process of the water treatment unit 231 scaling due to divalent cations can be prevented, and thus, a nanofiltration process and an antiscalant process necessary for removing divalent ions before concentrating the concentrated water can be omitted.
  • the electric energy charged in the seawater battery unit 211 is supplied to the desalination process unit 214 and can be used as an energy source of the desalination process unit 214.
  • the desalination unit 230 for hydrogen production includes a concentrated water treatment unit 231, a concentrated water pretreatment unit 232, and a chlorine-alkali processing unit 233.
  • the concentrated water treatment unit 231 receives the first concentrated water from which the divalent cations have been removed, and water-treats the concentrated water into the second concentrated water and the second produced water through an evaporation process.
  • the second concentrated water is preferably concentrated to a salinity (24 to 26% NaCl) sufficient to generate hydrogen gas in a chlorine-alkali processing unit 233 to be described later through an evaporation process.
  • the second concentrated water has a higher salinity than the first concentrated water.
  • the second concentrated water is supplied to the chlorine-alkali processing unit 233 after the pH is adjusted in the concentrated water pretreatment unit 232.
  • the second production water is stored in the production water storage tank 271.
  • the evaporation process may be performed by selecting any one of a film evaporation process (MD), a multistage evaporation process (MSF), or a multiple effect evaporation process (MED).
  • MD film evaporation process
  • MSF multistage evaporation process
  • MED multiple effect evaporation process
  • the concentrated water pretreatment unit 232 adjusts the pH of the second concentrated water to a pH lower than that of the second concentrated water by adding hydrochloric acid to the second concentrated water.
  • Hydrochloric acid is a chemical used to control the pH of concentrated water. Hydrochloric acid can be produced from chlorine gas and hydrogen gas generated in the chlorine-alkali process unit 233.
  • the pH of the second concentrated water is known, so that the second concentrated water reacts with the chlorine gas in the chlorine-alkali processing unit 233 to obtain hypochlorous acid (HClO). ) And other compounds.
  • the internal space of the chlorine-alkali processing unit 233 is divided into an anode portion 234 and a cathode portion 235 by a separator.
  • An anode 234a is installed in the anode part 234.
  • a cathode 235a is installed in the cathode portion 235.
  • the anode 234a and the cathode 235a are electrically connected.
  • the chlorine-alkali processing unit 233 electrolyzes concentrated water through solar electric energy to produce chlorine gas at the anode 234 and produces hydrogen gas and sodium hydroxide at the cathode 235.
  • the anode part 234 is connected to the chlorine tank 273 and the concentrated water crystallization part 240.
  • the cathode part 235 is connected to the hydrogen tank 275 and the NaOH tank 277.
  • the process of producing chlorine gas in the anode part 234 of the chlorine-alkali process part 233 will be described as follows.
  • the power source used may be renewable energy of the energy supply unit 250.
  • the salt (NaCl) contained in the second concentrated water is separated into sodium ions and chlorine gas.
  • Sodium ions pass through the separation membrane partitioning the anode portion 234 and the cathode portion 235, and move from the anode portion 234 to the cathode portion 235.
  • Chlorine gas is collected and stored in the chlorine tank 273. Chlorine gas is supplied to the product water storage tank 271, and can be used as a chemical to disinfect the product water. In addition, chlorine gas can be used as a raw material for producing hydrochloric acid.
  • the present invention can disinfect the water produced by using the chlorine gas produced in the chlor-alkali processing unit 233 without using a separate chlorine chemical, and by producing hydrochloric acid itself, it is consumed to adjust the pH of the water treatment process. It can reduce the cost of chemical treatment.
  • the salinity is lowered.
  • concentrated water having a lower salinity than the second concentrated water is referred to as diluted concentrated water.
  • the diluted concentrated water is discharged from the anode part 234 to the concentrated water crystallization part 240.
  • the pH of the second product water is adjusted by sodium hydroxide, and is provided to the negative electrode part 235.
  • the second production water is fresh water treated by the concentration process unit 120.
  • the second product water is the electrolyte of the cathode 235a.
  • Sodium hydroxide is produced by the chlorine-alkali process unit 233.
  • the second product water is used as an electrolyte, and the product water is electrolyzed into hydrogen gas and a hydroxyl group (OH-) to produce hydrogen gas.
  • the formula for producing hydrogen gas is formula (2).
  • Hydrogen gas is collected in the cathode part 235 and stored in the hydrogen tank 275. Hydrogen gas can be used as hydrogen energy.
  • sodium hydroxide is produced by a chemical reaction between sodium ions decomposed in the salt of concentrated water and a hydroxyl group (OH-).
  • the formula for producing sodium hydroxide is Equation (3).
  • Sodium hydroxide is stored in the NaOH tank 277.
  • Sodium hydroxide is used as a chemical to adjust the pH of the product water flowing into the negative electrode part 235 of the chlorine-alkali process part 233 described above.
  • sodium hydroxide is used as a chemical agent to control the pH of concentrated water and/or produced water.
  • sodium hydroxide is added to the influent to increase the pH of the influent, thereby increasing the removal rate of specific substances such as boron or silica from the influent water passing through the reverse osmosis process, and carbon dioxide that has passed through the reverse osmosis process is converted into carbonate ions or bicarbonate ions. Alkalinity can be recovered by changing to.
  • sodium hydroxide is added to the production water having a low pH after mineral injection, so that corrosion of the pipe network through which the product water flows can be prevented.
  • the diluted concentrated water discharged from the chlorine-alkali processing unit 233 is discharged to the concentrated water crystallization unit 240.
  • the diluted concentrated water is concentrated water whose concentration is diluted while the second concentrated water is electrolyzed and chlorine gas escapes from the second concentrated water.
  • the salinity of the diluted concentrated water is lower than that of the second concentrated water.
  • the concentrated water crystallization unit 240 removes moisture from the diluted concentrated water through a crystallization process, and crystallizes the diluted concentrated water into salt (NaCl). In the crystallization process, the diluted concentrated water is heated, and the salt in the diluted concentrated water is crystallized while the water in the diluted concentrated water escapes as steam. The concentrated water crystallization unit 240 may cool the steam generated during the crystallization process to produce third product water. The third production water is stored in the production water storage tank 271.
  • the crystallized salt (NaCl) can be recycled or treated as waste.
  • the present invention can prevent the destruction of the marine ecosystem due to the high concentration of concentrated water being discharged to the sea.
  • heating device 124 evaporation unit
  • cathode 161 NaOH tank
  • hydrochloric acid reaction unit 180 hydrochloric acid tank
  • cathode part 240 concentrated water crystallization part
  • the present invention is applicable to the field of producing hydrogen gas, which is a future energy source, from concentrated water discharged as wastewater during seawater desalination.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Electrochemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Nanotechnology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Automation & Control Theory (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)

Abstract

Un système de dessalement capable de produire de l'hydrogène selon un mode de réalisation de la présente invention comprend: une unité de traitement de dessalement dans laquelle de l'eau d'entrée est préparée en eau produite et en eau concentrée par traitement de l'eau par l'intermédiaire d'un processus d'osmose inverse; et une unité de traitement chlore-alcali ayant un espace interne délimité dans une partie anode et une partie cathode, l'eau concentrée étant fournie dans la partie anode, et l'eau produite étant fournie dans la partie cathode; l'unité de traitement chlore-alcali, par l'utilisation d'énergie électrique solaire, génère de préférence du chlore gazeux à partir d'un sel de l'eau concentrée par l'intermédiaire d'une réaction chimique dans la partie anode en utilisant l'eau concentrée en tant qu'électrolyte et génère de l'hydrogène gazeux et de l'hydroxyde de sodium par une réaction chimique dans la partie cathode à l'aide de l'eau produite en tant qu'électrolyte.
PCT/IB2020/054866 2019-03-25 2020-05-22 Système de dessalement capable de produire de l'hydrogène WO2020194284A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP20776475.4A EP3848331A4 (fr) 2019-03-25 2020-05-22 Système de dessalement capable de produire de l'hydrogène

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
KR1020190033654A KR102207458B1 (ko) 2019-03-25 2019-03-25 수소 생산가능한 담수시스템
KR10-2019-0033654 2019-03-25

Publications (1)

Publication Number Publication Date
WO2020194284A1 true WO2020194284A1 (fr) 2020-10-01

Family

ID=72610298

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/IB2020/054866 WO2020194284A1 (fr) 2019-03-25 2020-05-22 Système de dessalement capable de produire de l'hydrogène

Country Status (3)

Country Link
EP (1) EP3848331A4 (fr)
KR (1) KR102207458B1 (fr)
WO (1) WO2020194284A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112266054A (zh) * 2020-10-12 2021-01-26 益生瑞(上海)生物科技有限公司 一种适合家庭和医院各种消毒的酸性氧化电位水发生器

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR102442583B1 (ko) * 2021-04-14 2022-09-13 대우조선해양 주식회사 해수전지를 적용한 선박평형수 처리 시스템 및 운영 방법
CN113105058A (zh) * 2021-04-23 2021-07-13 广东闻扬环境科技有限公司 海水淡化零排放及资源回收利用工艺
US20230057182A1 (en) * 2021-08-18 2023-02-23 Austin J. Shields Produced water treatment with co2 absorption
KR20240061997A (ko) 2022-11-01 2024-05-08 주식회사 삼원카본써큘레이션 이산화탄소를 용해한 해수와 전기투석을 이용한 수소 생산 시스템 및 방법

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20110015354A (ko) * 2009-08-07 2011-02-15 배오성 그린에너지를 이용하여 해수를 가성소다와 담수로 분리하는 방법 및 장치
KR101206582B1 (ko) * 2010-06-28 2012-11-29 효성굿스프링스 주식회사 해수담수화를 위한 보론 제거 장치 및 방법
KR20130134078A (ko) * 2012-05-30 2013-12-10 한국해양과학기술원 해수 전기분해 알칼리 수로부터 마그네슘염과 칼슘염을 포함한 미네랄 염의 분리 및 이를 이용한 미네랄음료의 제조방법
KR101526299B1 (ko) 2014-05-26 2015-06-08 두산중공업 주식회사 플랜트-정삼투 하이브리드 담수화 시스템 및 방법
WO2016047257A1 (fr) * 2014-09-26 2016-03-31 株式会社日本トリム Dispositif de production d'eau électrolysée et appareil équipé de celui-ci pour fabriquer l'eau pour préparer un dialysat
KR20160087791A (ko) * 2014-03-27 2016-07-22 한양대학교 산학협력단 해수 농축수 전기분해를 통한 NaOH 회수장치 및 회수방법

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH06269777A (ja) * 1993-03-16 1994-09-27 Asahi Glass Co Ltd 造水プロセス
US6261464B1 (en) * 1999-05-25 2001-07-17 Miox Corporation Portable water disinfection system
US20110155665A1 (en) * 2008-06-11 2011-06-30 The Regents Of The University Of California Method and System for High Recovery Water Desalting
KR20130086717A (ko) * 2012-01-26 2013-08-05 삼성전자주식회사 전해 환원수 제조 장치 및 그 제어 방법
JP5865495B2 (ja) * 2012-07-06 2016-02-17 株式会社日立製作所 塩排水の処理方法及び装置
US9818496B2 (en) * 2014-08-18 2017-11-14 De Nora Permelec Ltd Method for treating tritium-water-containing raw water
KR101851645B1 (ko) * 2016-04-29 2018-06-07 국민대학교산학협력단 결정화장치가 결합된 막증류 수처리 장치 및 이를 이용한 유가자원 회수방법
WO2019036676A1 (fr) * 2017-08-18 2019-02-21 The Regents Of The University Of California Voies faciles, à faible énergie pour la production de sels de calcium et de magnésium hydratés à partir de déchets industriels alcalins

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20110015354A (ko) * 2009-08-07 2011-02-15 배오성 그린에너지를 이용하여 해수를 가성소다와 담수로 분리하는 방법 및 장치
KR101206582B1 (ko) * 2010-06-28 2012-11-29 효성굿스프링스 주식회사 해수담수화를 위한 보론 제거 장치 및 방법
KR20130134078A (ko) * 2012-05-30 2013-12-10 한국해양과학기술원 해수 전기분해 알칼리 수로부터 마그네슘염과 칼슘염을 포함한 미네랄 염의 분리 및 이를 이용한 미네랄음료의 제조방법
KR20160087791A (ko) * 2014-03-27 2016-07-22 한양대학교 산학협력단 해수 농축수 전기분해를 통한 NaOH 회수장치 및 회수방법
KR101526299B1 (ko) 2014-05-26 2015-06-08 두산중공업 주식회사 플랜트-정삼투 하이브리드 담수화 시스템 및 방법
WO2016047257A1 (fr) * 2014-09-26 2016-03-31 株式会社日本トリム Dispositif de production d'eau électrolysée et appareil équipé de celui-ci pour fabriquer l'eau pour préparer un dialysat

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112266054A (zh) * 2020-10-12 2021-01-26 益生瑞(上海)生物科技有限公司 一种适合家庭和医院各种消毒的酸性氧化电位水发生器

Also Published As

Publication number Publication date
KR20200115747A (ko) 2020-10-08
EP3848331A1 (fr) 2021-07-14
KR102207458B1 (ko) 2021-01-26
EP3848331A4 (fr) 2022-07-20

Similar Documents

Publication Publication Date Title
WO2020194284A1 (fr) Système de dessalement capable de produire de l'hydrogène
WO2016047901A1 (fr) Procédé et appareil de traitement d'eaux usées industrielles de type à réutilisation des ressources faisant appel à un agent oxydant généré par l'utilisation des eaux usées
WO2013019004A2 (fr) Appareil de production d'hypochlorite de sodium
CN101475276B (zh) 氧化铁生产废水的处理方法
WO2012161537A2 (fr) Appareil de traitement de l'eau et procédé de commande d'appareil de traitement de l'eau
CN110606612A (zh) 一种煤焦化高盐废水资源化处理工艺
WO2017043722A1 (fr) Dispositif de réduction de contaminant
KR102328974B1 (ko) 수소 생산가능한 담수시스템
US7037481B2 (en) Production of ultra pure salt
WO2017043741A1 (fr) Appareil de dessalement et procédé de dessalement l'utilisant
KR101436138B1 (ko) 해수전해 및 연료전지 복합시스템
WO2012165694A1 (fr) Appareil de stérilisation et procédé pour appareil de traitement d'eau
WO2016080783A1 (fr) Procédé de traitement d'eau de ballast par électrolyse de type à travers une ligne de dérivation et appareil pouvant traiter de l'eau douce et de l'eau de mer par stérilisation
WO2012091500A2 (fr) Appareil de traitement de l'eau et procédé de traitement de l'eau utilisant celui-ci
WO2022119407A1 (fr) Appareil d'électrolyse de l'eau de mer et système de liaison de pile à combustible à électrolyse de l'eau de mer le comprenant
CN105540958A (zh) 一种电厂废水零排放处理工艺
KR101256132B1 (ko) 컨테이너형 해수 담수화 장치
KR20140076540A (ko) 해수전해 및 연료전지 복합시스템
KR101339303B1 (ko) 전기응집과 전기분해를 이용한 불소가 함유된 질소 함유 병합처리방법
JP2012217943A (ja) 脱塩処理方法及び脱塩処理システム
TWI812844B (zh) 含有有機物及鈣的水的處理方法以及裝置
SU1318535A1 (ru) Способ электрохимической очистки сточных вод
WO2023090832A1 (fr) Appareil et procédé de traitement des eaux usées contenant des matières organiques non dégradables
WO2024049075A1 (fr) Système de traitement à décharge nulle d'eaux usées produites pendant le processus de recyclage de batteries aux ions de lithium usagées
WO2020017909A1 (fr) Procédé et appareil de recyclage d'eaux usées par osmose inverse

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 20776475

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: 2020776475

Country of ref document: EP

Effective date: 20210408

NENP Non-entry into the national phase

Ref country code: DE